EP3312153B1 - Methods for manufacturing aromatic hydrocarbon, paraxylene and terephthalic acid - Google Patents

Methods for manufacturing aromatic hydrocarbon, paraxylene and terephthalic acid Download PDF

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Publication number
EP3312153B1
EP3312153B1 EP16810696.1A EP16810696A EP3312153B1 EP 3312153 B1 EP3312153 B1 EP 3312153B1 EP 16810696 A EP16810696 A EP 16810696A EP 3312153 B1 EP3312153 B1 EP 3312153B1
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EP
European Patent Office
Prior art keywords
group
reaction
oxide
acid
temperature
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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EP16810696.1A
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German (de)
English (en)
French (fr)
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EP3312153A1 (en
EP3312153A4 (en
Inventor
Qi Song
Junlin ZHENG
Dejin Kong
Xuan XU
Xiaolan QI
Xiangdong Jiang
Deqin Yang
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Original Assignee
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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Publication date
Priority claimed from CN201510345846.3A external-priority patent/CN106316741B/zh
Priority claimed from CN201510345987.5A external-priority patent/CN106316766B/zh
Priority claimed from CN201510345823.2A external-priority patent/CN106316736A/zh
Priority claimed from CN201510345647.2A external-priority patent/CN106316740B/zh
Priority claimed from CN201510345806.9A external-priority patent/CN106256809B/zh
Priority claimed from CN201510345812.4A external-priority patent/CN106316735B/zh
Priority claimed from CN201510344592.3A external-priority patent/CN106316762B/zh
Priority claimed from CN201510345909.5A external-priority patent/CN106316738B/zh
Priority claimed from CN201510345824.7A external-priority patent/CN106316764B/zh
Application filed by China Petroleum and Chemical Corp, Sinopec Shanghai Research Institute of Petrochemical Technology filed Critical China Petroleum and Chemical Corp
Publication of EP3312153A1 publication Critical patent/EP3312153A1/en
Publication of EP3312153A4 publication Critical patent/EP3312153A4/en
Publication of EP3312153B1 publication Critical patent/EP3312153B1/en
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • C10G3/44—Catalytic treatment characterised by the catalyst used
    • C10G3/48—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/041—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/405—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
    • B01J29/44—Noble metals
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
    • B01J29/46—Iron group metals or copper
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J29/60—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the type L, as exemplified by patent document US3216789
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/7007—Zeolite Beta
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    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/7038—MWW-type, e.g. MCM-22, ERB-1, ITQ-1, PSH-3 or SSZ-25
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/7046—MTT-type, e.g. ZSM-23, KZ-1, ISI-4 or EU-13
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/80—Mixtures of different zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B01J37/0018—Addition of a binding agent or of material, later completely removed among others as result of heat treatment, leaching or washing,(e.g. forming of pores; protective layer, desintegrating by heat)
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/04—Mixing
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C07C1/207—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms from carbonyl compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C63/00—Compounds having carboxyl groups bound to a carbon atoms of six-membered aromatic rings
    • C07C63/14—Monocyclic dicarboxylic acids
    • C07C63/15—Monocyclic dicarboxylic acids all carboxyl groups bound to carbon atoms of the six-membered aromatic ring
    • C07C63/26—1,4 - Benzenedicarboxylic acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
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    • B01J2208/00548—Flow
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
    • C07C15/02—Monocyclic hydrocarbons
    • C07C15/04—Benzene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
    • C07C15/02—Monocyclic hydrocarbons
    • C07C15/06—Toluene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
    • C07C15/02—Monocyclic hydrocarbons
    • C07C15/067—C8H10 hydrocarbons
    • C07C15/08—Xylenes
    • C—CHEMISTRY; METALLURGY
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    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of rare earths
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    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C07C2523/24—Chromium, molybdenum or tungsten
    • C07C2523/28—Molybdenum
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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    • C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C07C2523/24—Chromium, molybdenum or tungsten
    • C07C2523/30—Tungsten
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    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • C07C2527/02—Sulfur, selenium or tellurium; Compounds thereof
    • C07C2527/053—Sulfates or other compounds comprising the anion (SnO3n+1)2-
    • C—CHEMISTRY; METALLURGY
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    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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    • C07C2527/06—Halogens; Compounds thereof
    • C07C2527/133—Compounds comprising a halogen and vanadium, niobium, tantalium, antimonium or bismuth
    • C—CHEMISTRY; METALLURGY
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    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
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    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1014—Biomass of vegetal origin
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    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/30—Aromatics
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • the present invention relates to a process for producing aromatics, in particular a process for producing BTX aromatics with a high yield of carbon.
  • the present invention further relates to a process for producing p-xylene and terephthalic acid based on the process for producing aromatics.
  • Aromatics are important fundamental raw materials for petrochemical industry, which are widely used in the fields of polyester, chemical fiber, rubber and the like. Benzene, toluene, and xylene are the three most widely used aromatics, which are generalized as light aromatics or BTX aromatics.
  • BTX aromatics the three most widely used aromatics, which are generalized as light aromatics or BTX aromatics.
  • the worldwide aromatic production depends mainly on the non-renewable fossil resource, whilst the production cost of aromatics is more and more increased due to the limited reserve and non-renewability of the fossil resource.
  • the increasing exploitation and utilization of fossil resource result in abundant discharge of greenhouse gases, leading to more and more severe environmental problems. Therefore, developing the technique of producing aromatics (especially BTX aromatics) from renewable resources is of importance.
  • JP 2010 202548 describes an apparatus for producing levulinic acid from biomass wherein biomass, and acid catalyst and water are reacted in a reactor under heating.
  • the inventors of the present invention deem it desirable to develop a process for producing aromatics, which shows improved biomass utilization efficiency and thus achieves improved yield of carbon for aromatics (in particular improved yield of carbon for BTX aromatics), when being used, for example, during the conversion from biomass material to aromatics.
  • the inventors of the present invention have discovered through hard study that the problems present in the prior art above can be solved by using a specific oxygen-containing compound as a platform compound in a process for producing aromatics using biomass material as a raw material, and thus have achieved the present invention.
  • the present invention involves the following aspects of contents.
  • the process for producing aromatics according to the present invention can, e.g., during the conversion process from biomass to aromatics, increase the carbon availability, reduce the proportion of carbon in the biomass material converted into gaseous carbon and carbon deposition, increase the yield of carbon for aromatics (in particular the yield of carbon for BTX aromatics) and finally increase the selectivity to BTX aromatics.
  • the yield of carbon as BTX aromatics can be up to 93% or more, with a minimum of 30% or more, and the selectivity to BTX aromatics can be up to 95% or more, using the process for producing aromatics according to the present invention.
  • the various ranges cited in the specification each comprise the terminals thereof, unless otherwise specified.
  • a range, one or more preferable ranges, or a plurality of preferable upper limit values and preferable lower limit values are disclosed for an amount, a concentration or any other value or parameter, they should be deemed as disclosing all ranges formed with arbitrary pairs of any upper limits or preferable values of the ranges with any lower limits or preferable values of the ranges, despite these value pairs being disclosed one by one or not.
  • any hydrocarbon or any group derived from a hydrocarbon having 3 or more carbon atoms should be understood to mean same with or without modification by a prefix of "n-".
  • propyl is generally understood to represent n-propyl
  • butyl is generally understood to represent n-butyl.
  • conversion, yield and selectivity denote respectively a single-pass conversion, a single-pass yield and a single-pass selectivity.
  • phrase "optionally substituted” denotes being optionally substituted by one or more (e.g., 1-3, 1-2 or 1) substituents selected from the group consisting of C 1-6 linear or branched alkyl optionally substituted by one or more carboxyl or hydroxyl, C 2-6 linear or branched alkenyl optionally substituted by one or more carboxyl or hydroxyl, C 2-6 linear or branched alkynyl optionally substituted by one or more carboxyl or hydroxyl, C- 3-10 cycloalkyl optionally substituted by one or more carboxyl or hydroxyl, C- 6-10 aryl optionally substituted by one or more carboxyl or hydroxyl, carboxyl and hydroxyl.
  • substituents selected from the group consisting of C 1-6 linear or branched alkyl optionally substituted by one or more carboxyl or hydroxyl, C 2-6 linear or branched alkenyl optionally substituted by one or more carboxyl or hydroxyl, C 2-6 linear
  • halogen denotes fluorine, chlorine, bromine and iodine.
  • One embodiment according to the present invention provides a process for producing aromatics, comprising a step of contacting an oxygen-containing raw material with an aromatization catalyst to produce aromatics, under aromatization reaction conditions (sometimes called as a contact step hereinafter).
  • the oxygen-containing raw material has structural formula (I).
  • R 1 is selected from the group consisting of optionally substituted C 1-8 linear or branched alkyl and optionally substituted C 2-8 linear or branched alkenyl, preferably optionally substituted C 1-4 linear or branched alkyl, more preferably methyl.
  • R 2 is selected from the group consisting of hydrogen and optionally substituted C 1-10 linear or branched alkyl, preferably selected from the group consisting of hydrogen and optionally substituted C 1-5 linear or branched alkyl, more preferably hydrogen.
  • n is a positive integer of 1 to 6, preferably a positive integer of 1 to 4, more preferably 2.
  • the oxygen-containing raw material is levulinic acid.
  • the reaction temperature is generally 100 to 1000 degrees C, in particular 300 to 800 degrees C, preferably 300 to 650 degrees C.
  • the reaction pressure is generally 0.1 to 20.0 MPa (gage pressure), in particular 0.1 to 10.0 MPa (gage pressure), preferably 0.5 to 6.0 MPa (gage pressure).
  • the hydrogen pressure is 0.1 to 5 MPa, preferably 0.5 to 4 MPa(gage pressure).
  • the WHSV of the oxygen-containing raw material is generally 0.1 to 20 hour -1 , in particular 0.3 to 10 hour -1 , preferably 0.5 to 5 hour -1 .
  • the oxygen-containing raw material is derived from a biomass material.
  • the biomass material can comprise those conventionally used to produce aromatics in the art, specifically, e.g., xylitol, glucose, cellobiose, cellulose, hemicellulose and lignin. These biomass materials can be used alone, or can be used as a combination of two or more thereof.
  • paper manufacture sludge, waste paper, bagasse, glucose, wood, corn cob, corn stover and straw stover can be specifically provided as further examples of the biomass material.
  • biomass materials can be used alone, or can be used as a combination of two or more thereof.
  • the content of cellulose is generally 30-99%, the content of hemicellulose is generally 0-50%, and the content of lignin is generally 0 or 1-40%, by weight percent.
  • the method for deriving the oxygen-containing raw material using a biomass material as raw material is not restricted specifically, while those conventionally known in the art can be used.
  • the method for derivation can comprise, for instance, a step of catalytically converting the biomass material (e.g., hydrolysis deoxidation, catalytic hydrolysis of inorganic acid, catalytic hydrolysis of organic acid, catalytic hydrolysis of solid acid, catalytic hydrolysis of molecular sieve, supercritical hydrolysis, catalytic partial oxidation or catalysis with metal chloride) to produce the oxygen-containing raw material (in particular levulinic acid) (e.g., see, Direct conversion of cellulose to levulinic acid and gamma-valerolactone using solid acid catalysts, Catal.
  • the biomass material e.g., hydrolysis deoxidation, catalytic hydrolysis of inorganic acid, catalytic hydrolysis of organic acid, catalytic hydrolysis of solid acid, catalytic hydrolysis of molecular sieve, supercritical
  • the aromatization catalyst is one or more selected from molecular sieve, solid super acid and composite metal oxide. These aromatization catalysts can be used alone, or can be used as a combination of two or more thereof.
  • examples of the aromatization catalyst can comprise preferably molecular sieve.
  • the molecular sieve is ZSM-type molecular sieve, which is M/ZSM-5. These molecular sieves can be used alone, or can be used as a combination of two or more thereof. These molecular sieves can be used directly as a commercially available product or can be produced according to a method known from prior art.
  • the molecular sieve is used in the form of a molecular sieve composition A, comprising: a1) 20 to 80 parts by weight of the molecular sieve, b1) 20 to 80 parts by weight of a binder, and c1) 0 to 10 parts by weight of an auxiliary.
  • the molecular sieve composition A comprises: a1) 30 to 70 parts by weight of the molecular sieve, b1) 30 to 70 parts by weight of a binder, and c1) 0.01 to 10 parts by weight (or 0.01 to 6 parts by weight) of an auxiliary.
  • the molecular sieve is used in the form of a molecular sieve composition B, comprising: a2) 90 to 99.99 parts by weight of the molecular sieve, and c2) 0.01 to 10 parts by weight of an auxiliary.
  • the molecular sieve composition B comprises: a2) 95 to 99.99 parts by weight of the molecular sieve, and c2) 0.01 to 5 parts by weight of an auxiliary.
  • these molecular sieve compositions can be used directly as a commercially available product or can be produced according to a method known from prior art.
  • a method of producing the molecular sieve composition the following method can be mentioned, for example: mixing and kneading molecular sieve, binder and, if needed, extrusion aid, pore-expanding agent and water to provide a mixture, extruding and shaping, followed by drying at a temperature of 100-200 degree Celsius for 1-24 h, and calcining at a temperature of 400-700 degree Celsius for 1-10 h.
  • extrusion aid can comprise those conventionally used in the art, such as sesbania powder, polyethylene glycol or sodium carboxymethylcellulose; while examples of the pore-expanding agent can comprise those conventionally used in the art, such as citric acid, oxalic acid or ethylenediamine tetraacetic acid and the like.
  • the extrusion aid and pore-expanding agent are added in a total amount not greater than 10wt% of the total weight of the mixture.
  • acid can also be added during shaping.
  • the acid can comprise inorganic acid, acetic acid or an aqueous solution thereof, in particular an aqueous solution of nitric acid,
  • the aqueous solution of acid is added in an amount of 50-90wt% of the total weight of the mixture.
  • the auxiliary can be incorporated during the production of the molecular sieve composition or after the production of the molecular sieve composition; or alternatively can be incorporated firstly into the molecular sieve followed by producing the molecular sieve composition using the thus obtained molecular sieve, without specific restriction thereto.
  • a method of incorporating the auxiliary can comprise those methods conventionally used in the art, in particular ion-exchange method or immersion method.
  • auxiliary is generally used in the form of a precursor.
  • examples of the precursor of metal auxiliary can comprise nitrate, sulfate, acetate or chloride salt of the metal; the examples the precursor of boron auxiliary can comprise boric acid or borax; while examples of the precursor of phosphorus auxiliary can comprise diammonium phosphate.
  • examples of the binder can comprise those binders conventionally used in the art for producing a molecular sieve composition, more specifically, for example, silica sol, pseudo-boehmite, alumina, acid treated clay, kaolin, montmorillonite and bentonite, in particular alumina (in particular ⁇ -alumina), pseudo-boehmite and montmorillonite.
  • binders can be used alone, or can be used as a combination of two or more thereof.
  • examples of the auxiliary can comprise Na, Ca, K, Be, Mg, Ba, V, Nb, Cr, Mo, W, Mn, Re, Fe, Co, Ni, Cu, Zn, Ga, Ru, Pd, Pt, Ag, B, Al, Sn, P, Sb, La and Ce, in particular Ca, K, Mg, Cr, Mo, Fe, Ni, Cu, Zn, Ga, Ru, Pd, Pt, Ag, B, Sn, P, La and Ce.
  • These auxiliaries can be used alone, or can be used as a combination of two or more thereof.
  • the auxiliary is preferably Zn, Ga, Sn or a combination thereof.
  • the molecular sieve is M/ZSM-5, wherein M is selected from the group consisting of Zn, Ga, Sn or a combination thereof.
  • M is selected from the group consisting of Zn, Ga, Sn or a combination thereof.
  • the molecular sieve or a molecular sieve composition comprising the molecular sieve is especially useful as the aromatization catalyst.
  • the molecular sieves can be used directly as a commercially available product or can be produced according to a method known from prior art.
  • examples of the solid super acid can comprise those conventionally used as solid acid catalyst, more specifically, for example, Lewis acid supported solid super acid, solid super acid as inorganic metal salt/Lewis acid composite and solid super acid as sulfated metal oxide.
  • These solid super acids can be used alone, or can be used as a combination of two or more thereof.
  • These solid super acids can be used directly as a commercially available product or can be produced according to a method known from prior art.
  • the Lewis acid supported solid super acid comprises a support and a Lewis acid on the support.
  • the support can comprise solid oxide of an element from Group IIIA and solid oxide of an element from Group IVA of the periodic table of elements, in particular SiO 2 , B 2 O 3 and Al 2 O 3 .
  • These supports can be used alone, or can be used as a combination of two or more thereof.
  • Lewis acid can comprise halide of an element from Group VB, halide of an element from Group IIIA and halide of an element from Group VA of the periodic table of elements, in particular halide of an element from Group VB and halide of an element from Group VA of the periodic table of elements, more particularly PF 3 , AsF 3 , SbF 3 , BiF 3 , SbFs, TaF 3 , VF 3 and NbF 3 .
  • fluoride is preferably used as a halide.
  • These Lewis acids can be used alone, or can be used as a combination of two or more thereof.
  • examples of the Lewis acid supported solid super acid can comprise SbF 5 /SiO 2 -Al 2 O 3 , PF 3 /Al 2 O 3 -B 2 O 3 , AsF 3 /Al 2 O 3 -B 2 O 3 , SbF 3 /Al 2 O 3 -B 2 O 3 , BiF 3 /Al 2 O 3 -B 2 O 3 , TaF 3 /Al 2 O 3 -B 2 O 3 , VF 3 /Al 2 O 3 -B 2 O 3 and NbF 3 /Al 2 O 3 -B 2 O 3 .
  • These Lewis acid supported solid super acids can be used alone, or can be used as a combination of two or more thereof.
  • the Lewis acid in the Lewis acid supported solid super acid, is supported in an amount of 1 to 30wt%, preferably 1 to 15wt%, relative to the weight of the support.
  • the solid super acid as inorganic metal salt/Lewis acid composite is a composite consisting of an inorganic metal salt and a Lewis acid.
  • the inorganic metal salt can comprise inorganic acid salt of a metal element from Group IB, inorganic acid salt of a metal element from Group IIB, inorganic acid salt of a metal element from Group VII and inorganic acid salt of a metal element from Group VIII of the periodic table of elements.
  • examples of the inorganic acid salt can particularly comprise haloid acid salt, especially hydrochloride.
  • Examples of the Lewis acid can comprise halide of an element from Group VB, halide of an element from Group IIIA and halide of an element from Group VA of the periodic table of elements, in particular halide of an element from Group IIIA of the periodic table of elements.
  • chloride is preferably used as a halide.
  • These Lewis acids can be used alone, or can be used as a combination of two or more thereof.
  • the solid super acid as inorganic metal salt/Lewis acid composite is preferably AlCl 3 -CuCl 2 . These solid super acids as inorganic metal salt/Lewis acid composite can be used alone, or can be used as a combination of two or more thereof.
  • the weight ratio between the inorganic metal salt and the Lewis acid is 1-30: 100, preferably 1-15: 100.
  • examples of the metal oxide in the solid super acid as sulfated metal oxide, can comprise oxide of a metal element from Group IVB of the periodic table of elements (called as oxide A hereinafter), or oxide obtained by modifying the oxide A with a modifying element comprising a metal element from Group IIIA, a metal element from Group VIIB, a noble metal element from Group VIII, a base metal element from Group VIII, a metal element from Group VIB or lanthanide metal element of the periodic table of elements (called as oxide B hereinafter).
  • oxides can be used alone, or can be used as a combination of two or more thereof.
  • These modifying elements can be used alone, or can be used as a combination of two or more thereof.
  • Examples of the oxide A can comprise ZrO 2 , TiO 2 or a combination thereof.
  • Examples of the modifying element can comprise Fe, Pt, Re, Al, W, Cr, Mo, Mn or a combination thereof.
  • the metal element from Group IIIA of the periodic table of elements is generally present in the form of an oxide
  • the metal element from Group VIIB is generally present in the form of an oxide
  • the noble metal element from Group VIII is generally present in the form of a metal elementary substance
  • the base metal element from Group VIII is generally present in the form of an oxide
  • the metal element from Group VIB is generally present in the form of an oxide
  • the lanthanide metal element is generally present in the form of an oxide.
  • Examples of the solid super acid as sulfated metal oxide can particularly comprise SO 4 2- /ZrO 2 , S 2 O 8 2- /ZrO 2 , SO 4 2- /TiO 2 , SO 4 2- /ZrO 2 -Fe 3 O 4 , Pt/SO 4 2- /TiO 2 , SO 4 2- /TiO 2 -ZrO 2 , SO 4 2- /TiO 2 -Al 2 O 3 , SO 4 2- /TiO 2 -WO 3 , SO 4 2- /ZrO 2 -Fe 2 O 3 -Cr 2 O 3 , SO 4 2- /ZrO 2 -WO 3 , SO 4 2- /TiO 2 -MoO 3 and SO 4 2- /ZrO 2 -Fe 2 O 3 -MnO 2 .
  • the aforementioned solid super acids as sulfated metal oxide can be used alone, or can be used as a combination of two or more thereof.
  • the weight ratio of the modifying element in the form of oxide (calculated as oxide) to the oxide A is generally 0.1-25: 100, preferably 0.5-10: 100, and the weight ratio of the modifying element in the form of metal elementary substance (calculated as metal) to the oxide A is generally 0.1-15: 100, preferably 0.3-6: 100.
  • the metal oxide in the solid super acid as sulfated metal oxide, generally has a sulfated rate of 0.5-25wt%, preferably 1-8wt%,
  • the method of producing the solid super acid as sulfated metal oxide is not restricted specifically, for which those conventionally known in the art can be used, specifically, e.g., precipitation-immersion method (for example, see the document " Progress in SO42-/MxOy solid superacid catalysts, Applied Chemical Industry, 2014, vol43, 1879-1883 ").
  • the composite metal oxide is a composite oxide of oxide of a metal element from Group IVB of the periodic table of elements with another oxide (called as oxide D hereinafter).
  • oxide D another oxide
  • the oxide C can comprise ZrO 2 , TiO 2 or a combination thereof, in particular ZrO 2 .
  • oxide D comprise oxide of a metal element from Group IIIA, oxide of a metal element from Group VII, oxide of a metal element from Group VIB, of the periodic table of elements, and oxide of a lanthanide metal element, more specifically B 2 O 3 , Al 2 O 3 , MnO 2 , Cr 2 O 3 , CrO 3 , MoO 3 , WO 3 , La 2 O 3 and CeO 2 , in particular MnO 2 , MoO 3 , WO 3 , La 2 O 3 and CeO 2 .
  • These oxides D can be used alone, or can be used as a combination of two or more thereof.
  • the composite metal oxide can comprise a composite oxide of ZrO 2 with one or more oxides D selected from the group consisting of MnO 2 , Mo 2 O 3 , WO 3 , La 2 O 3 and CeO 2 .
  • the ratio of oxide C to oxide D is generally 60-99.9: 0.1-40, preferably 60-99: 1-40, calculated in parts by weight.
  • the composite metal oxide can be used directly as a commercially available product or can be produced according to a method known from prior art.
  • the method of producing the composite metal oxide can comprise immersion method or precipitation method. More specifically, for example, an immersion method comprises immersing tungsten, molybdenum, cerium, lanthanum or manganese as a saline solution onto zirconia, throwing away the spare liquid after 12 to 48 hours of immersion, drying at a temperature of 100 to 200 degree Celsius, evaporating out of water to leave the active components, followed by treatment by calcining and activating procedures to provide the composite metal oxide; or alternatively, a precipitation method comprises adding simultaneously an aqueous solution of metal salt of tungsten, molybdenum, cerium, lanthanum or manganese, an aqueous solution of a metal salt of zirconium and an aqueous ammonia as precipitant to generate a solid precipitation, washing, filtrating and drying the precipitation generated, and
  • the contact step can be carried out in one or more reactors.
  • the reactor can comprise bed reactor, in particular fixed bed reactor, fluidized bed reactor, ebullated bed reactor or a combination thereof.
  • the reactor can be operated in batched, or continuously, without specific restriction.
  • the contact step can be carried out under inert gas atmosphere or reducing gas atmosphere.
  • inert gas atmosphere can comprise N 2 , CO 2 , He, Ar or a combination thereof.
  • reducing gas atmosphere can comprise CO, H 2 or a combination thereof.
  • aromatics are produced as a product according to the aforementioned process for producing aromatics.
  • the content of BTX aromatics is 60% or more by weight of the total weight, in particular, benzene content being 5.0-10.0%, toluene content being 30.0-40.0%, xylene content being 28.0-40.0%, whilst the balance being non-aromatic hydrocarbons and heavy aromatics.
  • the heavy aromatics denote C9 and higher aromatics.
  • the present invention further relates to a process for producing p-xylene, comprising a step of producing aromatics according to the process for producing aromatics of the present invention; and a step of separating p-xylene from the aromatics.
  • the method of separating p-xylene from the aromatics is not specifically restricted, while those conventionally known in the art can be used directly.
  • terephthalic acid can be produced using p-xylene produced according to the present invention introduced above as a raw material.
  • the present invention further relates to a process for producing terephthalic acid, comprising a step of producing p-xylene according to the aforementioned process for producing p-xylene of the present invention; and a step of converting the p-xylene into terephthalic acid.
  • the method of converting p-xylene into terephthalic acid is not specifically restricted, while those conventionally known in the art can be used directly.
  • the yield of carbon as aromatics and the yield of carbon as BTX aromatics are used to illustrate the result of tests, wherein the yield of carbon as BTX aromatics is the main comparative indicator.
  • the yield of carbon as aromatics and the yield of carbon as BTX aromatics are calculated according to the formulae below.
  • the yield carbon as aromatics % weight of aromatics as a reaction product g / carbon weight of the oxygen-containing raw material as a reaction raw material ⁇ 100 %
  • the yield carbon as BTX aromatics % weight of BTX aromatics as a reaction product g / carbon weight of the oxygen-containing raw material as a reaction raw material ⁇ 100 %
  • An example for calculation is as follows: 100 g of levulinic acid is used as the oxygen-containing raw material, which comprises 51.7 g of carbon; then, if 38.8 g of aromatics is obtained after reaction, the yield of carbon as aromatics is 75%.
  • the 38.8 g of aromatics comprises 19.4 g of BTX aromatics, then the yield of carbon as BTX aromatics is 50%.
  • the raw material was 1kg of bagasse, comprising 52% of dry basis cellulose and 27% of hemicellulose.
  • the raw material was 1kg of pine saw dust, comprising 41.9% of dry basis cellulose and 22.8% of hemicellulose.
  • the raw material was 1 t of paper manufacture sludge, having a dry basis cellulose content of 61%.
  • the paper manufacture sludge was mixed under sufficient stirring with 3.5 t of 3% aqueous solution of sulfuric acid, stirred and reacted under 3.0 MPa at a temperature of 205 degree Celsius for 25 min to complete the acidolysis process.
  • the liquid phase product was separated to provide 275 kg of levulinic acid and 104.5 kg of formic acid. 104.5 kg of formic acid was decomposed to provide 4.5 kg of hydrogen.
  • the levulinic acid product obtained was further converted on an aromatization catalyst.
  • the catalyst contained 60% of L-type zeolite with a molar ratio of Si:Al of 35 and balance of alumina supporter.
  • the reaction was conducted at a temperature of 450 degree Celsius under a reaction pressure of 0.8 MPa and a space velocity of 0.5 h -1 .
  • the conversion of levulinic acid was 100%.
  • the hydrocarbon product was obtained in a total amount of 136.7 kg, with a composition showed in 1-3.
  • the content of aromatics was 125.5 kg, and benzene, toluene and xylene comprised 87.9% by weight of the product.
  • the raw material was 1 t of bagasse, having a dry basis cellulose content of 52% and a hemicellulose content of 27%.
  • the bagasse was comminuted sufficiently, mixed under stirring with 3.5 t of 1.5% aqueous solution of hydrochloric acid, then added with 1.2 kg of iron trichloride, and the mixed solution was reacted under 1.0 MPa at a temperature of 180 degree Celsius by microwave heating for 10 min to complete the acidolysis process.
  • the liquid phase product was separated to provide 248 kg of levulinic acid, 95 kg of formic acid and 135 kg of furfural. 95 kg of formic acid was decomposed to provide 4.1 kg of hydrogen.
  • the hydrogenation product of levulinic acid containing predominantly methyl tetrahydrofuran and the hydrogenation product of furfural predominantly containing methyl tetrahydrofuran were further converted on an aromatization catalyst.
  • the catalyst contained 80% of MCM-22 type zeolite (with a molar ratio of Si:Al of 32), 3% of SiO 2 and 17% of Al 2 O 3 .
  • the reaction was conducted at a temperature of 450 degree Celsius under a reaction pressure of 0.8 MPa and a space velocity of 0.5 h -1 .
  • the conversion of methyl tetrahydrofuran was 100%.
  • the hydrocarbon product was obtained in a total amount of 166.2 kg, with a composition showed in 1-4.
  • the raw material was 1 t of municipal waste paper, having a dry basis cellulose content of 92.1%.
  • the municipal waste paper was comminuted sufficiently, mixed under stirring with 3.5 t of 3.5% aqueous solution of sulfuric acid, then added with 13 kg of sodium sulfite, and the mixed solution was reacted under stirring under 3.0 MPa at a temperature of 205 degree Celsius for 30 min to complete the acidolysis process.
  • the liquid phase product was separated to provide 464.4 kg of levulinic acid and 197.6 kg of formic acid. 197.6 kg of formic acid was decomposed to provide 8.5 kg of hydrogen.
  • the levulinic acid was further converted on an aromatization catalyst.
  • the catalyst contained 60% of ZSM-5 (a molar ratio of Si:Al of 38), 10% of ZSM-23 type zeolite (a molar ratio of Si:Al of 25) and 30% of SiO 2 .
  • the reaction was conducted at a temperature of 450 degree Celsius under a reaction pressure of 0.8 MPa and a space velocity of 0.5 h -1 .
  • the conversion of levulinic acid was 100%.
  • the hydrocarbon product was obtained in a total amount of 213.0 kg, with a composition showed in 1-5.
  • the content of aromatics was 187.5 kg, and benzene, toluene and xylene comprised 86.3% by weight of the product.
  • the raw material was 1 t of pine saw dust, having a dry basis cellulose content of 41.9% and a hemicellulose content of 22.8%.
  • the pine saw dust was comminuted sufficiently, mixed under stirring with 3.5 t of 2.8% aqueous solution of sulfuric acid, and the mixed solution was reacted under stirring under 3.0 MPa at a temperature of 205 degree Celsius for 40 min to complete the acidolysis process.
  • the liquid phase product was separated to provide 184 kg of levulinic acid, 75.6 kg of formic acid and 102 kg of furfural. 75.6 kg of formic acid was decomposed to provide 3.3 kg of hydrogen.
  • the furfural was hydrogenated on a 30% CuO-20% Cr 2 O 3 -50% SiO 2 precipitation type catalyst, with a reaction pressure of 2.0 MPa, a reaction temperature of 180 degree Celsius, a molar ratio of hydrogen/furfural of 10, and a space velocity of furfural of 0.5 h -1 , resulting in a conversion of furfural of 99%, and a selectivity to 2-methyl tetrahydrofuran of 92.1%.
  • 102 kg of furfural generated 79 kg of methyl tetrahydrofuran.
  • the hydrogen used for hydrogenations of levulinic acid and furfural was obtained from the decomposition of formic acid.
  • the product containing predominantly levulinic acid and the hydrogenation product of furfural predominantly containing methyl tetrahydrofuran were further converted on an aromatization catalyst.
  • the catalyst contained 60% of ZSM-23 type zeolite (with a molar ratio of Si:Al of 25), 2.5% of CeO 2 and 37.5% of Al 2 O 3 .
  • the reaction was conducted at a temperature of 480 degree Celsius under a reaction pressure of 0.8 MPa and a space velocity of 0.5 h -1 .
  • the conversion of levulinic acid and methyl tetrahydrofuran was each 100%.
  • the hydrocarbon product was obtained in a total amount of 124 kg, with a composition showed in 1-6.
  • the content of aromatics was 124 kg, and benzene, toluene and xylene comprised 90.0% by weight of the product.
  • the total amount of hydrogen created was 2.4 kg, the yield of carbon as aromatics was 73.9%, and the yield of carbon as BTX aromatics was 62.5%.
  • Table 1-6 composition of the aromatization product Non-aromatic hydrocarbons Benzene Toluene Ethylbenzene P-xylene M-xylene O-xylene C9 aromatics C 10 + aromatics Composition/wt% 11.5 8.3 31.8 4.7 8.3 17.5 8.9 7.2 1.8 Output/KG 14.5 10.4 39.8 5.9 10.4 21.9 11.2 9.0 2.2
  • the raw material was 1 t of cellulose, having a dry basis cellulose content of 98.3%.
  • the cellulose was mixed under stirring with 3.5 t of 3.7% aqueous solution of sulfuric acid.
  • the mixed solution was stirred under 3.0 MPa at a temperature of 205 degree Celsius for 30 min to complete the acidolysis process.
  • the liquid phase product was separated to provide 511 kg of levulinic acid and 194 kg of formic acid. 194 kg of formic acid was decomposed to provide 8.3 kg of hydrogen.
  • the levulinic acid product obtained was further converted on an aromatization catalyst.
  • the catalyst contained 60% of ZSM-5 type zeolite (with a molar ratio of Si:Al of 25), 10% of ⁇ -type zeolite (with a molar ratio of Si:Al of 60), 8% of ZrO 2 and 22% of Al 2 O 3 .
  • the reaction was conducted at a temperature of 430 degree Celsius under a reaction pressure of 0.8 MPa and a space velocity of 1.0 h -1 .
  • the conversion of levulinic acid was 100%.
  • the hydrocarbon product was obtained in a total amount of 233 kg, with a composition showed in 1-7.
  • the raw material was 1 t of paddy straw, having a dry basis cellulose content of 42.5% and a dry basis hemicellulose content of 18.7%.
  • the straw was comminuted sufficiently, 2.8kg of tin tetrachloride was added, mixed under stirring with 5 t of 3.2% aqueous solution of sulfuric acid, and the mixed solution was reacted under stirring under 2.0 MPa at a temperature of 205 degree Celsius for 30 min to complete the acidolysis process.
  • the liquid phase product was separated to provide 169 kg of levulinic acid, 70.3 kg of formic acid and 83.1 kg of furfural. 70.3 kg of formic acid was decomposed to provide 3 kg of hydrogen.
  • the product predominantly comprising methyl tetrahydrofuran and levulinic acid was further converted on an aromatization catalyst.
  • the catalyst contained 40% of ZSM-5 type zeolite (with a molar ratio of Si:Al of 25), 20% of ZSM-11 type zeolite (with a molar ratio of Si:Al of 30) and 40% of Al 2 O 3 .
  • the reaction was conducted at a temperature of 460 degree Celsius under a reaction pressure of 1.0 MPa and a space velocity of 3.0 h -1 .
  • the conversion of levulinic acid was 100%, and the conversion of methyl tetrahydrofuran was 100%.
  • the hydrocarbon product was obtained in a total amount of 101.9 kg, with a composition showed in 1-8.
  • the raw material was 1 t of corrugated paper, having a dry basis cellulose content of 83.5%.
  • the corrugated paper was comminuted, mixed under stirring with 5 t of 3.0% aqueous solution of sulfuric acid, then added with 13 kg of sodium chloride, and the mixed solution was reacted under stirring under 1.5 MPa at a temperature of 205 degree Celsius for 60 min to complete the acidolysis process.
  • the liquid phase product was separated to provide 387.1 kg of levulinic acid and 197.6 kg of formic acid. 197.6 kg of formic acid was decomposed to provide 6.6 kg of hydrogen.
  • the levulinic acid was further converted on an aromatization catalyst.
  • the catalyst contained 60% of ZSM-5 (a molar ratio of Si:Al of 38), 20% of ZSM-5 type zeolite (a molar ratio of Si:Al of 150) and 20% of Al 2 O 3 .
  • the reaction was conducted at a temperature of 450 degree Celsius under a reaction pressure of 0.8 MPa and a space velocity of 0.5 h -1 .
  • the conversion of levulinic acid was 100%.
  • the hydrocarbon product was obtained in a total amount of 176.2 kg, with a composition showed in 1-9.
  • the content of aromatics was 172.7 kg, and benzene, toluene and xylene comprised 65.5% by weight of the product.
  • the raw material was 1 t of bagasse, having a dry basis cellulose content of 52%.
  • the bagasse was comminuted sufficiently, mixed under stirring with 3.5 t of 1.5% aqueous solution of hydrochloric acid, then added with 1.2 kg of iron trichloride, and the mixed solution was reacted under 1.0 MPa at a temperature of 180 degree Celsius by microwave heating for 10 min to complete the acidolysis process.
  • the liquid phase product was separated to provide 210 kg of levulinic acid and 96.6 kg of formic acid.
  • Aromatization catalyst 80 g of ZSM-5 having a ratio of Si:Al of 50 was mixed with 20 g of pseudo-boehmite, 3.9 g of sesbania powder was added, and mixed homogeneously. Then, 45 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, and extruded as a strip. The catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 500 degree Celsius for 2 h, to provide a molecular sieve catalyst.
  • the levulinic acid-containing stream was further converted on an aromatization catalyst.
  • the reaction was conducted at a temperature of 450 degree Celsius under a reaction pressure of 1.0 MPa and a space velocity of 1.5 h -1 .
  • the conversion of levulinic acid was 100%.
  • the hydrocarbon product was obtained in a total amount of 102kg, with a composition showed in II-1.
  • the content of aromatics was 88.3kg, benzene, toluene and xylene comprised 85.6% by weight of the product, and the yield of carbon as aromatics was 81.3%.
  • the raw material was 1 t of pine saw dust, having a dry basis cellulose content of 41.9%.
  • the pine saw dust was comminuted sufficiently, mixed under stirring with 3.5 t of 2.8% aqueous solution of sulfuric acid, and the mixed solution was reacted under stirring under 3.0 MPa at a temperature of 205 degree Celsius for 40 min to complete the acidolysis process.
  • the liquid phase product was separated to provide 184 kg of levulinic acid and 84.0 kg of formic acid.
  • the levulinic acid-containing stream was further converted on an aromatization catalyst.
  • the reaction was conducted at a temperature of 420 degree Celsius under a reaction pressure of 1.5 MPa and a space velocity of 1.0 h -1 .
  • the conversion of levulinic acid was 100%.
  • the hydrocarbon product was obtained in a total amount of 76.2kg, with a composition showed in II-2.
  • the content of aromatics was 66.4kg, benzene, toluene and xylene comprised 84.6% by weight of the product, and the yield of carbon as aromatics was 69.8%.
  • the raw material was 1 t of municipal waste paper, having a dry basis cellulose content of 92.1%.
  • the municipal waste paper was comminuted sufficiently, mixed under stirring with 3.5 t of 3.5% aqueous solution of sulfuric acid, then added with 13 kg of sodium sulfite, and the mixed solution was reacted under stirring under 3.0 MPa at a temperature of 205 degree Celsius for 30 min to complete the acidolysis process.
  • the liquid phase product was separated to provide 435.5 kg of levulinic acid and 199.4 kg of formic acid.
  • the levulinic acid-containing stream was further converted on an aromatization catalyst.
  • the reaction was conducted at a temperature of 480 degree Celsius under a reaction pressure of 1.0 MPa and a space velocity of 2.0 h -1 .
  • the conversion of levulinic acid was 100%.
  • the hydrocarbon product was obtained in a total amount of 192.6kg, with a composition showed in II-3.
  • the content of aromatics was 162.2 kg, benzene, toluene and xylene comprised 82.7% by weight of the product, and the yield of carbon as aromatics was 72.3%.
  • the raw material was 1 t of cellulose, having a dry basis cellulose content of 98.3%.
  • the cellulose was mixed under stirring with 3.5 t of 3.7% aqueous solution of sulfuric acid.
  • the mixed solution was stirred under 3.0 MPa at a temperature of 205 degree Celsius for 30 min to complete the acidolysis process.
  • the liquid phase product was separated to provide 511 kg of levulinic acid and 235 kg of formic acid.
  • aromatization catalyst 30 g of L-type zeolite having a ratio of Si:Al of 50 was mixed with 20 g of ZSM-23 zeolite having a ratio of Si:Al of 35 and 30 g of pseudo-boehmite, 23 g of sesbania powder was added, and mixed homogeneously. Then, 36 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, and extruded as a strip. The catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 550 degree Celsius for 2 h, to provide an aromatization molecular sieve catalyst.
  • the levulinic acid-containing stream was further converted on the aromatization catalyst.
  • the reaction was conducted at a temperature of 450 degree Celsius under a reaction pressure of 1.5 MPa and a space velocity of 1.5 h -1 .
  • the conversion of levulinic acid was 100%.
  • the hydrocarbon product was obtained in a total amount of 210kg, with a composition showed in II-4.
  • the content of aromatics was 182.5 kg, benzene, toluene and xylene comprised 83.5% by weight of the product, and the yield of carbon as aromatics was 69.1%.
  • reaction substrate was levulinic acid with a WHSV of 0.3 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 and a temperature of 400 degree Celsius.
  • reaction result was qualitatively analyzed using mass spectra, and was quantitatively analyzed using chromatogram.
  • the conversion of substrate was 83%, the selectivity to BTX aromatics was 87%, and the yield of carbon as BTX aromatics was 72.2%.
  • reaction substrate was levulinic acid, with a WHSV of 3.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 20 ml min -1 and a temperature of 400 degree Celsius.
  • reaction result was qualitatively analyzed using mass spectra, and was quantitatively analyzed using chromatogram.
  • the conversion of substrate was 88%, the selectivity to BTX aromatics was 81%, and the yield of carbon as BTX aromatics was 71.3%.
  • reaction substrate was levulinic acid, with a WHSV of 5.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 20 ml min -1 and a temperature of 500 degree Celsius.
  • reaction result was qualitatively analyzed using mass spectra, and was quantitatively analyzed using chromatogram.
  • the conversion of substrate was 82%, the selectivity to BTX aromatics was 78%, and the yield of carbon as BTX aromatics was 64.0%.
  • 35 g of ZSM-5 having a ratio of Si:Al of 25 was mixed with 35 g of an auxiliary of ⁇ -alumina, 2.7 g of sesbania powder was added, and mixed homogeneously. Then, 48 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 500 degree Celsius for 2 h, to provide a molecular sieve catalyst C1.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being levulinic acid, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 95%, the selectivity to BTX aromatics was 87%, and the yield of carbon as BTX aromatics was 83%.
  • 35 g of ZSM-5 having a ratio of Si:Al of 50 was mixed with 35 g of pseudo-boehmite, 2.7 g of sesbania powder was added, and mixed homogeneously. Then, 48 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 500 degree Celsius for 2 h, to provide a molecular sieve catalyst C2.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being levulinic acid, a WHSV of 3.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 450 degree Celsius. After reaction, the conversion of the reaction substrate was 96%, the selectivity to BTX aromatics was 86%, and the yield of carbon as BTX aromatics was 83%.
  • 35 g of ZSM-5 having a ratio of Si:Al of 150 was mixed with 35 g of pseudo-boehmite, 2.7 g of sesbania powder was added, and mixed homogeneously. Then, 48 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 500 degree Celsius for 2 h, to provide a molecular sieve catalyst C3.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being levulinic acid, a WHSV of 2.5 hour -1 , a hydrogen pressure of 4.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 550 degree Celsius. After reaction, the conversion of the reaction substrate was 99%, the selectivity to BTX aromatics was 89%, and the yield of carbon as BTX aromatics was 88%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being levulinic acid, a WHSV of 5.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 30 ml min -1 , and a temperature of 380 degree Celsius. After reaction, the conversion of the reaction substrate was 96%, the selectivity to BTX aromatics was 83%, and the yield of carbon as BTX aromatics was 80%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 0.3 hour -1 , a hydrogen pressure of 3.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 450 degree Celsius. After reaction, the conversion of the reaction substrate was 99%, the selectivity to BTX aromatics was 94%, and the yield of carbon as BTX aromatics was 93%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 4.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 480 degree Celsius. After reaction, the conversion of the reaction substrate was 96%, the selectivity to BTX aromatics was 86%, and the yield of carbon as BTX aromatics was 83%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being ethyl levulinate, a WHSV of 2.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 450 degree Celsius. After reaction, the conversion of the reaction substrate was 92%, the selectivity to BTX aromatics was 83%, and the yield of carbon as BTX aromatics was 76%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being ethyl levulinate, a WHSV of 4.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 450 degree Celsius. After reaction, the conversion of the reaction substrate was 99%, the selectivity to BTX aromatics was 81%, and the yield of carbon as BTX aromatics was 80%.
  • 35 g of ZSM-5 having a ratio of Si:Al of 100 was mixed with 35 g of an auxiliary of ⁇ -alumina, 2.7 g of sesbania powder was added, and mixed homogeneously. Then, 48 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 500 degree Celsius for 2 h, to provide a molecular sieve catalyst C9.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 5.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 350 degree Celsius. After reaction, the conversion of the reaction substrate was 89%, the selectivity to BTX aromatics was 83%, and the yield of carbon as BTX aromatics was 74%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 430 degree Celsius. After reaction, the conversion of the reaction substrate was 81%, the selectivity to BTX aromatics was 87%, and the yield of carbon as BTX aromatics was 70%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 0.3 hour -1 , a hydrogen pressure of 2.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 450 degree Celsius. After reaction, the conversion of the reaction substrate was 93%, the selectivity to BTX aromatics was 78%, and the yield of carbon as BTX aromatics was 73%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 94%, the selectivity to BTX aromatics was 79%, and the yield of carbon as BTX aromatics was 74%.
  • Y having a ratio of Si:Al of 8 80 g was mixed with 20 g of pseudo-boehmite, 3.9 g of sesbania powder was added, and mixed homogeneously. Then, 68.6 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 500 degree Celsius for 2 h, to provide a molecular sieve catalyst C13.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 470 degree Celsius. After reaction, the conversion of the reaction substrate was 86%, the selectivity to BTX aromatics was 87%, and the yield of carbon as BTX aromatics was 75%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 430 degree Celsius. After reaction, the conversion of the reaction substrate was 91%, the selectivity to BTX aromatics was 82%, and the yield of carbon as BTX aromatics was 75%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 88%, the selectivity to BTX aromatics was 77%, and the yield of carbon as BTX aromatics was 68%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 84%, the selectivity to BTX aromatics was 88%, and the yield of carbon as BTX aromatics was 74%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 81%, the selectivity to BTX aromatics was 82%, and the yield of carbon as BTX aromatics was 66%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 0.3 hour -1 , a hydrogen pressure of 0.3 MPa, a flow rate of 50 ml min -1 , and a temperature of 480 degree Celsius. After reaction, the conversion of the reaction substrate was 83%, the selectivity to BTX aromatics was 89%, and the yield of carbon as BTX aromatics was 74%.
  • Comparative example VI-1 was practiced to illustrate the synthesis of a catalyst comprising 5A type as the main active component, the preparation of catalyst and the properties thereof for aromatization of levulic acid.
  • the specific reactants formulation and the experimental method were provided as follows: 35 g of 5A molecular sieve having a ratio of Si:Al of 2 was mixed with 35 g of an auxiliary of ⁇ -alumina, 2.7 g of sesbania powder was added, and mixed homogeneously. Then, 48 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 500 degree Celsius for 2 h, to provide a molecular sieve catalyst C5A.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being levulinic acid, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , a temperature of 400 degree Celsius. After reaction, calculation of the reaction result showed that the conversion of the reaction substrate was 35%, the selectivity to BTX aromatics was 17%, and the yield of carbon as BTX aromatics was 6%.
  • reaction substrate was levulinic acid with a WHSV of 0.3 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 and a temperature of 400 degree Celsius.
  • reaction result was qualitatively analyzed using mass spectra, and was quantitatively analyzed using chromatogram.
  • the conversion of substrate was 99%, the selectivity to BTX aromatics was 93%, and the yield of carbon as BTX aromatics was 92%.
  • reaction substrate was levulinic acid with a WHSV of 3.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 20 ml min -1 and a temperature of 400 degree Celsius.
  • reaction result was qualitatively analyzed using mass spectra, and was quantitatively analyzed using chromatogram.
  • the conversion of substrate was 89%, the selectivity to BTX aromatics was 87%, and the yield of carbon as BTX aromatics was 77%.
  • 35 g of ZSM-5 having a ratio of Si:Al of 25 was mixed with 35 g of an auxiliary of ⁇ -alumina, 2.7 g of sesbania powder was added, and mixed homogeneously. Then, 48 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, calcined at a temperature of 500 degree Celsius for 2 h, then was immersed with equal-volume of Zn(NO 3 ) 2 in an addition amount of Zn of 1%, and was dried and calcined to provide a molecular sieve catalyst.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being levulinic acid, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 450 degree Celsius. After reaction, the conversion of the reaction substrate was 99%, the selectivity to BTX aromatics was 93%, and the yield of carbon as BTX aromatics was 92%.
  • 35 g of ZSM-5 having a ratio of Si:Al of 50 was mixed with 35 g of pseudo-boehmite, 2.7 g of sesbania powder was added, and mixed homogeneously. Then, 48 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, calcined at a temperature of 500 degree Celsius for 2 h, then was immersed with equal-volume of Cu(NO 3 ) 2 in an addition amount of Cu of 2%, and was dried and calcined to provide a molecular sieve catalyst C2.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being levulinic acid, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 420 degree Celsius. After reaction, the conversion of the reaction substrate was 92%, the selectivity to BTX aromatics was 95%, and the yield of carbon as BTX aromatics was 87%.
  • 35 g of ZSM-5 having a ratio of Si:Al of 150 was mixed with 35 g of pseudo-boehmite, 2.7 g of sesbania powder was added, and mixed homogeneously. Then, 48 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, during which kneading Ga(NO 3 ) 2 was added in an addition amount of Ga of 1% based on the weight of the molecular sieve, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 500 degree Celsius for 2 h, to provide a molecular sieve catalyst C3.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being levulinic acid, a WHSV of 1.5 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50ml min -1 , and a temperature of 420 degree Celsius.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being levulinic acid, a WHSV of 1.0 hour -1 , a hydrogen pressure of 4.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 470 degree Celsius. After reaction, the conversion of the reaction substrate was 98%, the selectivity to BTX aromatics was 87%, and the yield of carbon as BTX aromatics was 85%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 3.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 380 degree Celsius. After reaction, the conversion of the reaction substrate was 91%, the selectivity to BTX aromatics was 74%, and the yield of carbon as BTX aromatics was 90%.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, calcined at a temperature of 500 degree Celsius for 2 h, then was immersed with equal-volume of lanthanum nitrate in an addition amount of La of 1%, and was dried and calcined to provide a molecular sieve catalyst C6.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 5.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 480 degree Celsius. After reaction, the conversion of the reaction substrate was 96%, the selectivity to BTX aromatics was 89%, and the yield of carbon as BTX aromatics was 85%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being ethyl levulinate, a WHSV of 3.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 550 degree Celsius. After reaction, the conversion of the reaction substrate was 99%, the selectivity to BTX aromatics was 83%, and the yield of carbon as BTX aromatics was 82%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being ethyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 5.0 MPa, a flow rate of 20 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 99%, the selectivity to BTX aromatics was 91%, and the yield of carbon as BTX aromatics was 90%.
  • ZSM-5 powder having a ratio of Si:Al of 50 was weighed and ion exchanged in a 180 ml of aqueous solution comprising lanthanum nitrate and cerous nitrate at a temperature of 90 degree Celsius for 2 h.
  • the metal contents of La and Ce in the solution are respectively 1 wt% of the solid molecular sieve powder. Drying was conducted after exchange, and 35 g of ZSM-5 having a ratio of Si:Al of 50 was mixed with 35 g of an auxiliary of ⁇ -alumina, 2.7 g of sesbania powder was added, and mixed homogeneously.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 2.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 450 degree Celsius. After reaction, the conversion of the reaction substrate was 96%, the selectivity to BTX aromatics was 89%, and the yield of carbon as BTX aromatics was 85%.
  • 35 g of Y molecular sieve having a ratio of Si:Al of 6 was mixed with 35 g of an auxiliary of ⁇ -alumina, 2.7 g of sodium carboxymethylcellulose was added, and mixed homogeneously. Then, 48 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, during which kneading copper nitrate and zinc nitrate were added in an addition amount of copper and zinc of respectively 1% and 1% by weight based on the weight of the molecular sieve solid, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 500 degree Celsius for 2 h, to provide a molecular sieve catalyst C10.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 450 degree Celsius.
  • the conversion of the reaction substrate was 91%
  • the selectivity to BTX aromatics was 81%
  • the yield of carbon as BTX aromatics was 74%.
  • Y molecular sieve having a ratio of Si:Al of 8 60 g was mixed with 40 g of an auxiliary of ⁇ -alumina, 3.9 g of sesbania powder was added, and mixed homogeneously. Then, 68.6 g of an aqueous solution of phosphoric acid comprising 5.5 wt% of phosphoric acid was added, mixed and kneaded for shaping, during which kneading silver nitrate was added in an addition amount of Ag of 1% based on the weight of the molecular sieve solid, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 500 degree Celsius for 2 h, to provide a molecular sieve catalyst C11.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 3.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 450 degree Celsius. After reaction, the conversion of the reaction substrate was 93%, the selectivity to BTX aromatics was 88%, and the yield of carbon as BTX aromatics was 82%.
  • 60 g Y molecular sieve having a ratio of Si:Al of 8 was weighed and ion exchanged in a 180 ml of aqueous solution comprising nickel nitrate at a temperature of 90 degree Celsius for 2 h.
  • the metal content of Ni in the solution is 5 wt% of the solid molecular sieve. Drying was made after exchange, 70 g of Y molecular sieve having a ratio of Si:Al of 8 was mixed with 30 g of pseudo-boehmite, 3.9 g of sesbania powder was added, and mixed homogeneously.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 94%, the selectivity to BTX aromatics was 89%, and the yield of carbon as BTX aromatics was 84%.
  • 180 g Y molecular sieve having a ratio of Si:Al of 8 was weighed and ion exchanged in a 180 ml of aqueous solution comprising gallium nitrate at a temperature of 90 degree Celsius for 2 h.
  • the metal content of Ga in the solution is 2 wt% of the solid molecular sieve. Drying was made after exchange, 80 g of Y molecular sieve having a ratio of Si:Al of 8 was mixed with 20 g of pseudo-boehmite, 3.9 g of sesbania powder was added, and mixed homogeneously.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 4.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 86%, the selectivity to BTX aromatics was 87%, and the yield of carbon as BTX aromatics was 75%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being methyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 91%, the selectivity to BTX aromatics was 82%, and the yield of carbon as BTX aromatics was 75%.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 460 degree Celsius. After reaction, the conversion of the reaction substrate was 98%, the selectivity to BTX aromatics was 87%, and the yield of carbon as BTX aromatics was 85%.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, calcined at a temperature of 500 degree Celsius for 2 h, then was immersed with equal-volume of niobium nitrate in an addition amount of Nb of 1%, and was dried and calcined to provide a molecular sieve catalyst C16.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 94%, the selectivity to BTX aromatics was 88%, and the yield of carbon as BTX aromatics was 83%.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, calcined at a temperature of 500 degree Celsius for 2 h, then was immersed with equal-volume of ammonium tungstate in an addition amount of W of 1%, and was dried and calcined to provide a molecular sieve catalyst C17.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 91%, the selectivity to BTX aromatics was 82%, and the yield of carbon as BTX aromatics was 75%.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, calcined at a temperature of 500 degree Celsius for 2 h, then was immersed with equal-volume of manganous nitrate in an addition amount of Mn of 3%, and was dried and calcined to provide a molecular sieve catalyst C18.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being butyl levulinate, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , and a temperature of 400 degree Celsius. After reaction, the conversion of the reaction substrate was 93%, the selectivity to BTX aromatics was 89%, and the yield of carbon as BTX aromatics was 83%.
  • Comparative example VIII-1 was practiced to illustrate the synthesis of a catalyst comprising 5A type as the main active component, the preparation of catalyst and the properties thereof for aromatization of levulinic acid.
  • the specific reactants formulation and the experimental method were provided as follows: 35 g of 5A molecular sieve having a ratio of Si:Al of 2 was mixed with 35 g of an auxiliary of ⁇ -alumina, 2.7 g of sesbania powder was added, and mixed homogeneously. Then, 48 g of an aqueous solution of nitric acid comprising 5.5 wt% of nitric acid was added, mixed and kneaded for shaping, and extruded as a strip.
  • the catalyst precursor obtained was dried at a temperature of 120 degree Celsius for 8 h, and calcined at a temperature of 500 degree Celsius for 2 h, to provide a molecular sieve catalyst C5A.
  • the catalyst was evaluated for activity on a fixed bed, under reaction conditions of: 3 g of catalyst, the reaction substrate being levulinic acid, a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 , a temperature of 400 degree Celsius. After reaction, calculation of the reaction result showed that the conversion of the reaction substrate was 35%, the selectivity to BTX aromatics was 17%, and the yield of carbon as BTX aromatics was 6%.
  • reaction substrate was levulinic acid with a WHSV of 0.3 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 50 ml min -1 and a temperature of 450 degree Celsius.
  • reaction result was qualitatively analyzed using mass spectra, and was quantitatively analyzed using chromatogram.
  • the conversion of substrate was 97%, the selectivity to BTX aromatics was 93%, and the yield of carbon as BTX aromatics was 90%.
  • reaction substrate was levulinic acid with a WHSV of 3.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 20 ml min -1 and a temperature of 400 degree Celsius.
  • reaction result was qualitatively analyzed using mass spectra, and was quantitatively analyzed using chromatogram.
  • the conversion of substrate was 86%, the selectivity to BTX aromatics was 86%, and the yield of carbon as BTX aromatics was 74%.
  • reaction substrate was methyl acetobutyrate with a WHSV of 0.8 hour -1 , a hydrogen pressure of 4.0 MPa, a flow rate of 40 ml min -1 and a temperature of 400 degree Celsius.
  • reaction result was qualitatively analyzed using mass spectra, and was quantitatively analyzed using chromatogram.
  • the conversion of substrate was 93%, the selectivity to BTX aromatics was 83%, and the yield of carbon as BTX aromatics was 77%.
  • reaction substrate was ethyl levulinate with a WHSV of 1.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 20 ml min -1 and a temperature of 500 degree Celsius.
  • reaction result was qualitatively analyzed using mass spectra, and was quantitatively analyzed using chromatogram.
  • the conversion of substrate was 99%, the selectivity to BTX aromatics was 83%, and the yield of carbon as BTX aromatics was 82%.
  • reaction substrate was methyl levulinate with a WHSV of 2.0 hour -1 , a hydrogen pressure of 1.0 MPa, a flow rate of 20 ml min -1 and a temperature of 380 degree Celsius.
  • reaction result was qualitatively analyzed using mass spectra, and was quantitatively analyzed using chromatogram.
  • the conversion of substrate was 87%, the selectivity to BTX aromatics was 83%, and the yield of carbon as BTX aromatics was 72%.

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EP16810696.1A 2015-06-19 2016-06-17 Methods for manufacturing aromatic hydrocarbon, paraxylene and terephthalic acid Active EP3312153B1 (en)

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CN201510345812.4A CN106316735B (zh) 2015-06-19 2015-06-19 生产芳烃的方法
CN201510345987.5A CN106316766B (zh) 2015-06-19 2015-06-19 芳构化的方法
CN201510345909.5A CN106316738B (zh) 2015-06-19 2015-06-19 生产芳烃的方法及该方法得到的组合物
CN201510345806.9A CN106256809B (zh) 2015-06-19 2015-06-19 生物质生产芳烃的方法及该方法得到的组合物
CN201510345824.7A CN106316764B (zh) 2015-06-19 2015-06-19 芳构化制芳烃方法
CN201510344592.3A CN106316762B (zh) 2015-06-19 2015-06-19 芳烃的生产方法
CN201510345647.2A CN106316740B (zh) 2015-06-19 2015-06-19 芳构化方法
CN201510345846.3A CN106316741B (zh) 2015-06-19 2015-06-19 芳构化合成芳烃的方法
CN201510345823.2A CN106316736A (zh) 2015-06-19 2015-06-19 芳构化生产芳烃的方法
PCT/CN2016/000315 WO2016201955A1 (zh) 2015-06-19 2016-06-17 芳香烃、对二甲苯和对苯二甲酸的制造方法

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